Methods of making pigmented filaments

ABSTRACT

Polymeric compositions include a nonaqueous additive system having dispersant-coated pigments physically dispersed in a liquid nonaqueous polymeric carrier which may be added directly to a melt flow of a polymeric host material. The additive system employed in the polymeric systems is most preferably in the form of a particulate paste which can be added in metered amounts (dosed) to a melt flow of the polymeric host material prior to being spun into filaments. By providing a number of additive systems having a number of different additive attributes, and controllably dosing one or more into the melt flow of host polymeric material, shaped objects of the polymeric material (e.g., melt-spun filaments) having different additive attributes may be produced on a continuous basis without shutting down the shaping operation.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional of, and claims priority benefits under 35 USC §120 from, commonly owned, U.S. patent application Ser. No. 09/075,169 filed on May 11, 1998 (now U.S. Pat. No. 6,232,371 B1), which in turn is a continuation-in-part of U.S. patent applications Ser. No. 08/810,197 (now U.S. Pat. No. 5,869,551), U.S. Ser. No. 08/810,196 (now U.S. Pat. No. 5,889,089), U.S. Ser. No. 08/810,198 (now U.S. Pat. No. 5,955,516), U.S. Ser. No. 08/811,058 (now U.S. Pat. No. 5,800,746), U.S. Ser. No. 08/811,061 (now U.S. Pat. No. 5,833,893) and U.S. Ser. No. 08/810,379 (now U.S. Pat. No. 5,834,089), each of which was filed on Mar. 3, 1997, and each claiming domestic priority benefits under 35 USC §119(e) from, U.S. Provisional Application Ser. No. 60/012,794 filed on Mar. 4, 1996, the entire content of each such application being expressly incorporated hereinto by reference.

FIELD OF INVENTION

The present invention relates generally to the field of thermoplastic polymeric materials containing one or more additives. In preferred exemplary embodiments, the present invention relates to synthetic filament additives (e.g., colorants) and to methods for incorporating such additives in melt flows of filament-forming thermoplastic polymeric materials prior to melt-spinning to form synthetic filaments therefrom.

BACKGROUND AND SUMMARY OF THE INVENTION

The incorporation of additives in so-called “neat” thermoplastic polymeric host materials (that is, polymeric materials containing no additives) so as to achieve desired physical properties is well known. Thus, the art has conventionally incorporated colorants, stabilizers, delusterants, flame retardants, fillers, antimicrobial agents, antistatic agents, optical brighteners, extenders, processing aids and other functional additives into polymeric host materials in an effort to “engineer” desired properties of the resulting additive-containing polymeric host material. Such additives are typically added any time prior to shaping of thepolymeric material, for example, by spinning or molding (e.g., extrusion, injection, or blow-molding) operations.

The incorporation of colorant additives in filaments formed by melt-spinning a polymeric material has presented unique challenges. For example, the amount of particulate pigment dispersed in a concentrate which is added to the polymeric material must be sufficiently high to impart satisfactory color density, but must not be so high as to interrupt the spinning process. One prior proposal for incorporating colorant additives in thermoplastic polymeric materials is disclosed in U.S. Pat. No. 5,236,645 to Frank R. Jones on Aug. 17, 1993 (the entire content of which is expressly incorporated hereinto by reference).

According to the Jones '645 patent, additives are introduced into a thermoplastic melt by feeding at least one additive in an aqueous vehicle containing a dispersant to form an aqueous additive stream to a vented extruder which is extruding a thermoplastic. The aqueous portion of the aqueous additive stream is thereby volatilized within the extruder and is removed therefrom via an extruder vent. As a result, a substantially homogeneous system containing the thermoplastic, dispersant and the additive is obtained which may thereafter be spun into a filament by melt-extrusion through filament-forming orifices in a spinneret associated with a spin pack assembly.

Although the techniques disclosed in the Jones '645 patent are entirely satisfactory, some further improvements to incorporating additives in a melt flow of thermoplastic polymeric materials would be desirable. For example, it would especially be desirable if the additive stream was non-aqueous as this would obviate the need for a vented extruder (i.e., since a volatilized aqueous portion of the additive stream would not then need to escape prior to melt-spinning). Furthermore, it is entirely possible that a non-aqueous additive stream could be introduced physically near or into the spin pack assembly where it can be mixed with a melt flow of the polymeric material immediately upstream of the spinneret orifices (and preferably downstream of the polymer filter section of the spin pack assembly) thereby bypassing the extruder. Such a possibility would then allow additive concentration and/or types to be changed on a continuous basis to produce sequential lengths of melt-spun filaments having desired, but different, properties and/or characteristics. That is, the upstream processing equipment, for example, the extruders and process piping, which supply the polymeric host material to the spin pack assembly would not necessarily need to be shut down for purposes of cleaning. Furthermore, by introducing a non-aqueous additive stream directly into the spin pack assembly, the flushing time would be relatively short thereby allowing, for example, quick color changes to occur from one filament production batch to another. It is towards providing such improvements that the present invention is directed.

Broadly, the present invention is embodied in a nonaqueous additive concentrate system for thermoplastic polymeric host materials which may be added directly to a melt flow of the polymeric material in metered amounts. More specifically, the additive concentrate system according to the present invention includes an additive which is dispersed in a liquid or liquefied nonaqueous carrier. The additive is most preferably in the form of a solid particulate pigment which is coated with a normally solid dispersant. The dispersant is preferably polymeric and substantially soluble in the carrier so as to form a solid pigment phase dispersed throughout a liquid or liquefied carrier phase. The additive concentrate system according to this invention is most preferably in the form of a flowable paste which can be added in metered amounts (dosed) to a melt flow of the polymeric material prior to being spun into filaments, for example near or into the spin pack assembly upstream of the assembly's filament-forming spinneret orifices.

In such a manner, therefore, synthetic filament batches having different additives may be produced sequentially on a continuous basis without costly equipment downtime. That is, the same spin pack assembly may be used to produce a first batch of filaments containing one type of additive during one production interval, and then used to produce a second batch of filaments containing a second type of additive during a succeeding production interval by changing the additive which is introduced into the filament-forming melt. Moreover, the time interval needed to change between different additives is relatively short since the additive system is most preferably introduced into the melt flow near or into the spin pack assembly which in turn reduces significantly the time needed to flush residual additive incorporated into the first batch of filaments. Production of different additive-containing filaments (e.g., filaments containing different colorants) is now possible in a relatively short period of time without stopping filament winding.

Thus, another aspect of this invention involves a method of continuously producing sequential lengths of different additive-containing filaments by continuously supplying a melt-spinnable polymeric host material to orifices of a spinneret and, during a first time interval, controllably dosing a concentrate system having one additive into the polymeric material to form a first polymeric mixture which is extruded through the spinneret orifices. Subsequently, during a second time interval, another concentrate system containing a different additive is controllably dosed into the polymeric material without disrupting the continuous supply of polymeric material to the spinneret orifices to form a second polymeric mixture which is extruded through the spinneret orifices.

During the change of additive concentrate, an intermediate time interval will be needed in order to flush the spinneret of residual amounts of the first additive concentrate. Thus, during the intermediate time intervals, an intermediate length of filaments will be produced which will change over the filament length from containing all of the first additive concentrate to containing all of the second additive concentrate. This intermediate length of filaments produced according to the present invention will be handled separately from the first and second lengths of production filaments. However, the amount of such intermediate length of filaments will be relatively small since, as noted above, the time interval needed to flush the spinneret of residual amounts of the first additive concentrate is relatively short.

Other advantages ensue from introducing the additive concentrate system to the polymeric host material within the spin pack assembly. For example, the spin pack assembly and its associated spinneret orifices may be so designed to form melt-spun multicomponent filaments (e.g., filaments having multiple domains of different polymer blends, colorants and/or other additives) such as those filaments disclosed in U.S. Pat. No. 5,162,074 to Hills (the entire content of which is expressly incorporated hereinto by reference) by splitting a melt-flow of polymeric host material into two or more subflows within the spin pack assembly. According to the present invention, therefore, the additive concentrate system may be introduced into the spin pack assembly and mixed with one or more of such subflows of polymeric host material without being mixed with other subflows so as to form multicomponent filaments. Therefore, while the discussion which follows emphasizes the production of filaments in which the additive concentrate system is substantially homogeneously mixed through the filament cross-section, it will be understood that the present invention is likewise applicable to the formation of multicomponent filaments whereby the additive concentrate system is substantially homogeneously mixed throughout one or more multiple polymeric domains in the filament cross-section without being present in the other domain(s) (e.g., as in core-sheath filaments, pie wedge filaments, side-by-side filaments and the like).

As noted above, significant processing flexibility ensues according to the present invention. Processing flexibility is the result of at least two features of the present invention. First, additive concentrate systems can be mixed above the spinneret with either the entire host polymer or only a portion of the host polymer. For example, a functional additive (e.g., an antistatic agent) concentrate system might be mixed with only a third of the host polymer such that a third of the filaments spun contain the antistatic agent and the remaining two-thirds do not.

Second, two or more additive concentrate systems can be mixed with the host polymer above the spinneret to achieve a single attribute in the fiber that is spun. For example, a yellow additive concentrate system and a blue additive concentrate system can be concurrently mixed with host polymer above the spinneret to provide a green fiber when the mixture is spun. There is no theoretical limit for the number of additive concentrate systems that can be mixed with the host polymer above the spinneret. The number of additive concentrate systems is limited only by the space available to inject the systems into the line. It is contemplated that the host polymer might also contain some additive prior to mixing above the spinneret.

These two features of the present invention are not mutually exclusive and great flexibility ensues from combining them. Using color as an example, either single color or multicolor yarn can be spun using the present invention. Single color yarn may be spun by mixing one or more color additive concentrate systems (e.g., a yellow system and blue system as exemplified above) with the entire host polymer such that a one color yarn (e.g., a multifilamentary yarn containing only green filaments) results.

Multicolor yarn (e.g., heather yarn) may be spun by selectively coloring separated portions of the host polymer and keeping each separated portion segregated until spun. For example, a portion of the host polymer might be colored with both the yellow and the blue additive systems to produce green filaments. Another portion of the host polymer might be colored with a red additive system to produce red filaments which are spun concurrently with the green filaments. The resulting multifilamentary yarn will therefore exhibit a heathered color due to the combination of individual red and green filaments present in the yarn.

The concepts above apply also to the spinning of filaments having multiple cross-sectional domains, such as core-sheath filaments, pie wedge filaments, side-by-side filaments and the like. Thus, for multidomain filaments, the additive concentrate system may be mixed with one or more split flows of the host polymer and then recombined with the remainder of the host polymer flow to achieve filaments having the additive present only in one or more of the cross-sectional domains.

When the additive is a colorant, therefore, a virtually unlimited number of multicolored, multidomain filaments can be produced. For example, only the core of a core-sheath filament may include one or more colorant additives which imparts to the fiber a color attribute that is visibly perceptible through the uncolored sheath. In this regard, it has been found that colorant additive(s) contained only in the core of a core-sheath multidomain filament results in a color intensity that is achieved with reduced colorant loading levels (e.g., between about 5 to about 10% less) as compared to filaments having the same colorant additive(s) homogeneously dispersed throughout the entire filament cross-section to achieve comparable color intensity.

Alternatively or additionally, the colorant additive may be present in the sheath of a core-sheath filament so as to achieve a color effect that is a combination of the core and sheath colors. Thus, by selectively choosing and incorporating colorants into the core and/or sheath, virtually any color attribute can be achieved for the resulting filament. Some particular combinations of colorants in both the core and sheath of a core-sheath filament may not necessarily result in a “pure” color combination of such colorants being realized for the filament. That is, the additive/subtractive effects of colorants in the core and sheath of core-sheath filaments are relatively complex and sometimes cannot be predicted with absolute certainty. However, routine experimentation with colorants in the core and/or sheath of core-sheath filaments will result in virtually an unlimited number of desired filament color attributes being obtained.

Other multiple domain filament combinations are envisioned, such as side-by-side domain filaments having different color attributes in each of the sides or pie wedge filaments whereby one or more of the wedges have the same or different color attributes. Such multiple domain filaments may be usefully employed to form heather yarns since the color additive-containing domains will visually present themselves at different locations along the length of the filaments when twisted (e.g., as may occur during yarn processing). Furthermore, the colorants and domains in which such colorants are present can be selected to achieve filaments which macroscopically appear to be uniformly colored.

Furthermore, although the additive concentrate systems of this invention may be metered (dosed) into the host polymer (whether in its entirety or in one or more of its split flows) at a substantially constant rate, periodic or continual variance of the dose rate is also envisioned. Thus, as noted briefly above, when changing from one filament recipe to another, one or more of the additive concentrates will need to be varied in order to switch filament production from a former recipe to the then current recipe. A random or constant dosage rate variance can also be practiced, however, in which case the resulting filaments will have more or less of the additive distributed along its length. When the additive is a colorant, such a technique allows filaments to be formed having a slub-like color appearance along its axial length which may be employed, for example, to produce yarns having a striated or marbled impression.

These and other aspects and advantages of this invention will become more clear after careful consideration is given to the following detailed description of the preferred exemplary embodiments thereof.

BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWING

Reference will hereinafter be made to the accompanying drawing wherein FIG. 1 is a schematic view of a filament melt-spinning apparatus in which the additive system of this invention may be added to a melt flow of polymeric material prior to spinning.

DETAILED DESCRIPTION OF THE PREFERRED EXEMPLARY EMBODIMENTS

To promote an understanding of the principles of the present invention, descriptions of specific embodiments of the invention follow and specific language describes the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended, and that such alterations and further modifications, and such further applications of the principles of the invention as discussed are contemplated as would normally occur to one ordinarily skilled in the art to which the invention pertains.

Thus, for example, while reference has been, and will hereinafter be, made to melt-spinning of filaments, it will be understood that other operations which serve to shape a melt of a polymeric material to a final form (e.g., extrusion or injection molding, blow-molding or the like) are contemplated. Furthermore, for ease of reference, the discussion which follows will emphasize the presently preferred embodiment of the invention in terms of incorporating colorants into polymeric materials, but the present invention can likewise be employed to incorporate virtually any other conventional additive as may be desired. In this regard, the term “pigment” as used herein and in the accompanying claims is meant to refer to virtually any material that may be added physically to a polymer melt flow, and thus generically encompasses colorant pigments which will be emphasized in the discussion which follows. Thus, suitable pigments which may be employed in the practice of this invention include solid and liquid colorants, stabilizers, delusterants, flame retardants, fillers, antimicrobial agents, antistatic agents, optical brighteners, extenders, processing aids and other functional additives.

As used herein and in the accompanying claims, the term “color” includes Munsell Values between about 2.5/ to about 8.5/ and Munsell Chromas greater than about /0.5. (Kelly et al, The ISCC-NBS Method of Designating Colors and a Dictionary of Color Names, National Bureau of Standards Circular 553, pp. 1-5 and 16 (1955), incorporated hereinto by reference.)

The term “normally solid” means a component which is physically substantially in a solid phase at normal ambient (room) temperatures of between about 20° C. to about 25° C. The term “normally liquid”, therefore, is meant to refer to a component which is physically substantially in a liquid phase when subjected to normal ambient (room) temperatures of between about 20° C. to about 25° C.

The term smelt processing temperature” is meant to refer to the temperature at which a normally solid thermoplastic material is processed in a melt phase and includes the temperatures at which such materials are extruded, molded or otherwise shaped when in a melt phase, in addition to the temperatures at which such materials are blended in a melt phase with other liquid or solid components. The melt processing temperature for a given thermoplastic material may be substantially at or somewhat greater than that material's melt temperature depending on the processing conditions that are desired.

The term “melt-processable” refers to any normally solid thermoplastic material that may be processed substantially in the melt phase and then resolidified at lower solidification temperatures following such melt-processing.

The term “water soluble” means a material that is solubilized substantially in contact with water to an extent of at least 90 wt. % by weight, and most preferably at least about 100 wt. %.

The host polymer in which the additive concentrate system of this invention may be incorporated includes any normally solid, melt-processable, synthetic thermoplastic polymer. The host polymer may thus be a polycondensate (polyamide, polyester, polyurethane), polyolefin, or any other such thermoplastic polymeric material that can be melt-processed at elevated melt-processing temperature and then resolidified at temperatures less than the melt-processing temperature. Most preferably, the host polymer is capable of being melt-processed into synthetic filaments (i.e., melt-spinnable). Exemplary polymers are polyamides such as poly(hexamethylene adipamide), polycaprolactam and polyamides of bis(4-aminocyclohexyl) methane and linear aliphatic dicarboxylic acids containing 9, 10 and 12 carbon atoms; copolyamides; polyester such as poly(ethylene)terephthalic acid and copolymers thereof; polyolefins such as polyethylene and polypropylene; and polyurethanes. Both heterogeneous and homogeneous mixtures of such polymers may also be used.

I. Additive Concentrate Preparation

As noted above, the additive concentrate system employed in the practice of the present invention is a dispersion of dispersant-coated pigment in a nonaqueous liquid or liquefied polymeric carrier. The pigment particles are physically homogeneously dispersed as “islands” throughout a “sea” of the dispersant component to form dispersant-laden pigment particles. These dispersant-laden pigment particles are, in turn, dispersed as “islands” throughout a “sea” of the carrier component.

A. The Additive Component

The most preferred additive that may be employed in the practice of this invention are those in the form of normally solid particulates that remain in a solid phase when subjected to the elevated melt-processing temperature of the thermoplastic host polymer (and thereby are present as solid particulates dispersed in the melt-processed, resolidified thermoplastic host polymer). Although a variety of pigments may be employed in the practice of the present invention, it is presently preferred that the pigment is a particulate pigment having a mean particle size of less than 10 μm, preferably less than about 5 μm, and most preferably between 0.1 μm to about 2 μm. The preferred pigment is a colorant which imparts a desired color to the host polymer when the additive concentrate system is incorporated thereinto. Most preferably, the pigment includes normally solid particulate colorant particles which remain solid at melt-processing temperatures of the thermoplastic host polymer.

B. The Dispersant Component

The additive concentrate system in accordance with the present invention will necessarily include a primary dispersant component, and optionally, a codispersant. The primary dispersant can be virtually any water soluble material that is normally solid when dehydrated and which is capable of coating the individual pigment particles. More specifically, the dispersant must coat the individual pigment particles in order to maintain particle-to-particle separation (i.e., prevent agglomeration) during mixing, particle size reduction (e.g., by bead-milling or other particle size reduction techniques) and processing (e.g., during dispersion of the dispersant-coated pigments into the carrier component). Most preferably, the primary dispersant is in a substantially liquid phase at melt-processing temperatures of the host polymer, and is thermally stable at such temperatures (i.e., does not significantly decompose at such melt-processing temperatures).

The primary dispersant must also be soluble in the host polymer at melt-processing temperatures to an extent of at least about 5 wt. %, and more preferably at least about 10 wt. % of dispersant in the host polymer, based on the total weight of the dispersant and host polymer. By the term “soluble” when used herein in reference to polymer-to-polymer blending is meant that, at the weight percent levels specified, one normally solid polymeric material may be melt-blended with the other polymeric material so as to form a polymeric alloy of the two polymeric components, whereby the presence of distinct regions, phases or domains of either one of the polymeric materials in the alloy cannot be detected visually under microscopic examination at a magnification of about 560x.

One particularly preferred technique to assist in the determination of whether a candidate primary dispersant and host polymer are soluble is to melt-extrude a dry blend of the host polymer and candidate dispersant in the desired amount of at least about 5 wt. %, and more preferably of at least about 10 wt. %. The resulting extrudate when resolidified may then be visually examined under a microscope to determine solubility in the manner noted previously.

However, the primary dispersant must be insoluble with the carrier material at the storage temperature of the additive concentrate system. By “storage temperature” as used herein is meant a temperature which is less than about the melt processing temperature of the host polymer minus 50° C.

Further qualitative tests on candidate primary dispersants may be performed in order to determine its suitability for use in the additive concentrate systems of this invention. For example, a primary dispersant chip containing dispersed pigment particles may be formed and tested through spin filters as described in the above-cited U.S. Pat. No. 5,236,645 to Jones. The results of this test provide an indication of whether the candidate dispersant can maintain pigment particle separation during melt-processing.

An aqueous dispersion of the candidate primary dispersant and pigment particles may also be allowed to stand at ambient temperatures to determine whether the dispersion is stable and/or whether a codispersant is necessary. Specifically, a codispersant may be needed if the dispersant-coated pigment particles settle and cannot readily be redispersed in the aqueous medium. As used herein, the term “stable” when referring to dispersions means that the dispersion either does not separate into a visually identifiable layers when allowed to stand for prolonged period of time without agitation, or if visually identifiable layers do form after standing for a prolonged time period, then a stable dispersion is such that the visually identifiable layers may be readily redispersed with one another by gentle agitation sufficient to impart laminar flow to the liquid for a time sufficient to achieve such homogenous redispersion. Furthermore, if spray-drying is employed to form dispersant-laden particles, a codispersant may be needed in the event such particles stick together (thereby possibly clogging the spray-drying equipment) over a range of spray-drying temperature profiles.

If used in the practice of this invention, the codispersant may be present in an amount up to about 20 wt. %, based on the total weight of the aqueous dispersion (i.e., the weight of the particulate additive, dispersant and codispersant components dispersed in an aqueous medium), and most preferably in the range between about 2.5 to about 7.5 wt. %. The amount of such codispersant, if used, will be dependent upon the components being processed and will be present in an amount sufficient to improve the spray-drying processability of the aqueous dispersion and/or improve the stability of the ultimate nonaqueous dispersion which includes the spray-dried dispersant-laden particulate additive.

Virtually any suitable codispersant which improves and/or alleviates the stability and/or processing difficulties noted above may be employed in the practice of the present invention. In this regard, one step in the selection of a codispersant is to evaluate the effect of a candidate codispersant material on the aqueous dispersion. Specifically, virtually any candidate codispersant material that improves the quality of the aqueous dispersion should improve the dispersion's stability. The dispersion viscosity may be monitored as a codispersant candidate material is added, the concentration of codispersant is optimized by minimizing the dispersion viscosity. Samples of the dispersant, pigment and codispersant dispersions may then be allowed to stand without agitation for evaluation of dispersion stability. To test for dispersion stability, dispersions need to stand with no agitation for a period of time sufficient to simulate the time that may pass between preparation and use for an actual nonaqueous dispersion. Thereafter, the dispersions are observed to determine their stability according to the definition stated above.

The aqueous dispersion of the candidate dispersant and the pigment particles may also be dried to ensure that the aqueous pigment dispersion can function to prepare a powder of dispersant-laden pigment particles. In this regard, during spray-drying as noted above, a codispersant may be necessary to prevent pigment particles from sticking together during the spray-drying process.

The codispersants that may be employed in the practice of the present invention include polyethylene glycol p-octyl phenyl ether (TRITON X-100 octyl phenyl ether, Aldrich Chemical Co., Inc.), polyoxypropylene/ethylene block copolymers (PLURONIC® 25R2 surfactants, BASF Corporation), alkoxylated diamines (TETRONIC® 150R1 surfactant, BASF Corporation), sodium lauryl sulfate and cationic dispersants (VARAQUAT 55 dispersants, Fibre Chemicals, Inc.). The codispersant, if present, is present in the additive concentrate system in an amount between about 2 to about 100 wt. % based on the weight of the pigment, and more preferably, between about 5 to about 45 wt. %.

A technique that may optionally or additionally be employed in the practice of this invention so as to stabilize a particle-containing liquid dispersion is to modify the dispersion's viscosity using so-called “viscosity builders” so that the pigment particles do not settle as rapidly. Some preferred viscosity builders include water soluble/dispersible polyesters and copolymers thereof, water soluble/dispersible vinyl polymers and copolymers thereof, water soluble/dispersible alkylene oxide polymers and copolymers thereof and water soluble/dispersible polyolefins and copolymers thereof. These preferred viscosity builders may be used singly or as a mixture of one or more of the same.

The preferred primary dispersants which may be employed in the practice of this invention, alone or in combination with one another and/or with the optional codispersants described above, are the water soluble/dispersible polymers as described in U.S. Pat. No. 3,846,507 (the entire content of which is expressly incorporated hereinto by reference). One particularly useful class of dispersants include sulphonated polyamide and sulphonated polyesters. For example, one specific preferred example of a sulphonated polyamide is a copolymer of polycaprolactam and/or caprolactam with hexamethylene-diamine, isophthalic acid and a sodium salt of sulfoisophthalic acid having a molecular weight of about 7,000, a specific gravity (H₂O=1) of about 1.1, a solubility in water of about 25% at 20° C. This preferred water soluble/dispersible polyamide copolymer dispersant is manufactured by BASF Corporation and will hereinafter be referenced as “C-68”.

Other useful dispersants that may be employed in the practice of this invention are water soluble/dispersible sulphonated polyesters. One particularly preferred sulphonated polyester which is completely dispersible in water is commercially available from Eastman Chemical Products, Inc., Kingsport, Tenn., under the product name “LB-100”. This preferred water soluble/dispersible polyester has a specific gravity (H₂O=1) of about 1.08, and is available commercially as a 30% solution of the polyester in water.

Other water soluble/dispersible polymers that may be useful in the practice of the present invention include, but are not limited to other water soluble/dispersible polyamides and copolymers thereof, water soluble/dispersible polyesters and copolymers thereof, water soluble/dispersible vinyl polymers and copolymers thereof, water soluble/dispersible alkylene oxide polymers and copolymers thereof and water soluble/dispersible polyolefins and copolymers thereof, as well as mixtures of the same. Other dispersants, like monomeric dispersants, may be suitable for use with the present invention.

One presently preferred technique for producing the additive dispersion of this invention uses as a starting material the aqueous dispersion formed according to the above-referenced Jones '645 patent. The aqueous dispersion may then be bead-milled and subjected to a spray drying operation so as to remove the aqueous component. The resulting dispersant-coated pigment granules (hereinafter more simply referred to as the “dispersible pigment granules”) are in powder form and have an average particle size of greater than about 5 μm. The dispersible pigment granules may then be mixed with a nonaqueous liquid polymeric carrier material. When dispersed into the polymeric host material, the dispersible pigment granules will break apart into average particle sizes of about 1 μm or less. In this way, maximum pigment loadings may be achieved without unduly increasing viscosity of the paste, while at the same time allowing the dispersible pigment granules to readily disperse in the polymeric host material at a size which does not affect adversely the spinning operation.

C. The Carrier Component

The carrier material can be virtually any material that is liquid at or below melt-spinning temperatures of the polymeric host material. Preferably, the carrier material is a polyamide or a polyester. The carrier material must also be compatible with the thermoplastic polymeric host material. That is, the carrier material is soluble in the host polymer at melt-processing temperatures to an extent of at least about 5 wt. %, and more preferably at least about 10 wt. % of carrier in the host polymer, based on the total weight of the carrier and host polymer. The carrier material must be liquid at or below about 200° C., and more preferably at or below about 150° C. The carrier material must also be thermally stable at melt processing temperature (i.e., showing substantially no cross-linkage and/or discoloration and/or decomposition which might cause fuming at the melt-processing die or spinneret).

When providing an additive concentrate system for incorporation into a nylon-6 polymeric host material, the presently preferred carrier is polycaprolactone since it is liquid at room temperatures (20° C.). However, as noted above, carriers that may be liquefied at elevated temperatures (e.g., less than about 200° C.) are also useable in the practice of this invention. For example, when providing an additive concentrate system for incorporation into a nylon-6 polymeric host material, it is also possible to use copolyamides having a melting point of less than about 200° C. One particularly preferred class of such copolyamides is commercially available under the trade name VESTAMELT® copolyamides from Huls America Inc. of Piscataway, N.J., with VESTAMELT® 722 copolyamide being particularly preferred.

One alternative technique to make the additive concentrate system according to this invention involves mixing the pigment, carrier and, if present, dispersant to form a nonaqueous paste in a one-step process thereby eliminating the need to prepare an aqueous dispersion which is subsequently spray dried. It is preferred that the dispersant, if present, and the carrier be premixed prior to addition of the pigment. The mixture may then be milled so as to obtain a paste which can be introduced directly into a melt flow of the polymeric host material.

The additive concentrate system of this invention may also be prepared by combining the pigment and the dispersant in a high-intensity mixer (e.g., a Henschel FM series mixer available commercially from Henschel Mixers America, Inc. of Houston, Tex.) until they are intimately mixed. Thereafter, the shear imparted by the mixer is reduced, and the required mass of carrier is added to yield the additive concentrate of this invention in paste form.

However formed, the additive concentrate system is most preferably in the form of a flowable paste having a viscosity during introduction into the polymeric host material ranging between about 500 cP to about 500,000 cP, and most preferably between about 1,500 cP to about 100,000 cP, at a temperature between about 20° C. to about 200° C. The dispersible additive may be maintained to within an acceptable viscosity range by application of heat (e.g., by keeping the dispersible additive in a suitable storage vessel which is jacketed with electrical resistance heaters and/or a heat transfer medium).

The additive concentrate system preferably contains pigment in an amount between about 5 to about 75 wt. %, more preferably between about 10 to about 65 wt. % based on the weight of the additive concentrate system. The additive concentrate system (the dispersible additive) itself is incorporated into the polymeric host material at levels between about 0.01 to about 15 wt. %, more preferably between about 0.05% and 10.0 wt. % based on the total weight of the polymeric host material and additive concentrate system. When. spray dried dispersible pigment granules are employed, they will preferably be present in the paste (that is, the dispersible pigment granules and the carrier material) so as to provide a solids content in the paste of at least about 50 wt. %, and more preferably at least about 57 wt. % or greater.

II. FILAMENT PRODUCTION

Accompanying FIG. 1 schematically depicts a filament spinning operation 10 by which additive concentrate systems may selectively be mixed with a melt flow of polymeric host material discharged from a conventional screw extruder 12 and supplied to an inlet of the spin pack assembly 14. More specifically, the polymeric host material is introduced into the upstream polymer filter section 14 a of the spin pack assembly before being extruded through orifices in the spinneret 14 b to form additive-containing filaments 16. Prior to reaching the spinneret 14 b, the polymeric host material may be distributed by a plurality of thin distribution plates 14 c in accordance with the above-noted U.S. Pat. No. 5,162,074 to William H. Hills, which may or may not have one or more static mixing plates, for example, as disclosed in U.S. Pat. No. 5,137,369 to John A. Hodan (the entire content of which is expressly incorporated hereinto by reference).

Batches of the additive concentrate systems in paste form are respectively held within portable tanks 18 a-18 d. In the accompanying FIG. 1, tanks 18 a-18 d are shown supported on wheeled carts 20 a-20 d, respectively, so as to permit each of the tanks 18 a-18 d to be replaced easily with stand-by tanks containing a fresh supply of the same or different additive concentrate system. However, other means can be employed which allow the tanks 18 a-18 d to be portable, such as inground or overhead conveyance systems, cranes and the like. Preferably, the additive concentrate system contained in each of the tanks 18 a-18 d is different—that is, tanks 18 a-18 d may each contain a different pigment or pigment mixture so that selective incorporation of each will result in the desired properties being achieved for the filaments 16.

Specifically, the tanks 18 a-18 c may each respectively contain dispersible colorant pigments corresponding to selected colors such as aqua, magenta and yellow, while tank 18 d may have a specially formulated tint color (e.g., white, black or the like) to achieve the desired. color hue, chroma and/or intensity. The differently colored additive concentrates held within the tanks 18 a-18 d may thus be volumetrically dosed or mixed with the polymeric host material so as to achieve a virtually unlimited number of resulting colors of the melt-spun filaments 16. In a like manner, other filament properties may be “engineered” by selective incorporation of other non-colorant pigments.

The carts 20 a-20 d also support a primary pump 22 a-22 d and a metering pump 24 a-24 d, respectively. The pumps 22 a-22 d and 24 a-24 d are most preferably gear-type pumps which serve to force the additive concentrate system paste through respective supply lines 26 a-26 d to the spin pack assembly 14. More specifically, the primary pumps 22 a-22 d serve to maintain a relatively constant input pressure to the immediately downstream respective metering pump 24 a-24 d. The primary pumps 22 a-22 d are therefore relatively larger capacity as compared to their respective downstream metering pump 24 a-24 d.

The additive concentrate system paste within each of the tanks 18 a-18 d is maintained under constant agitation in order to prevent sedimentation of the pigment therein. Such agitation may be accomplished by a motor-driven mixer 26 a-26 d and/or via recycle lines 28 a-28 d (and/or lines 30 a-30 d). Of course, if the pigment is in solution with the carrier, then such agitation may not be needed.

The metering pumps 24 a-24 d are variable speed so as to achieve variable volumetric outputs within their respective capacity range stated previously. The speed of the metering pumps 24 a-24 d is most preferably controlled by a logic programmable controller LPC. Specifically, for a given “recipe” (for example, a desired color for the pigmented filaments 16) input into the controller LPC, appropriate outputs will be issued to one or more of the metering pumps 24 a-24 d to cause them to operate at a speed to achieve a desired volumetric output for their particular dispersible additive. Thus, it will be recognized that for certain desired colors, some but not all of the metering pumps 24 a-24 d will be supplying paste from their respective tanks 18 a-18 d to the spin pack assembly 14 and/or may be operated at different speeds to achieve different volumetric outputs. Suffice it to say, that by selectively controlling the operation of the metering pumps 24 a-24 d and, when operated, their respective speed (and hence their respective volumetric outputs), selective volumetric paste doses can be continuously supplied to the spin pack assembly 14 where the respective additive concentrate systems will be homogeneously mixed with the melt flow of polymeric host material being fed by the extruder 12 via line 32.

The respective speed of one or more of the metering pumps 24 a-24 d may also be varied continually to thereby respectively vary the volumetric dose of one or more of the colorant systems over time. Such speed (dose) variance will thereby cause more or less additive concentrate system being incorporated into the filament per unit time where results in a filament having varying amounts of the additive per unit length. In the context of color additives, such speed variance may be employed so as to form filaments having a randomly striated or marbled color appearance.

The additive concentrate pastes from lines 26 a-26 d are most preferably introduced directly into the spin pack assembly 14 at a location corresponding to the distribution/mixing section 14 c—that is, at a location downstream of the polymer filter 14 a, but upstream of the spinneret 14 b. In this manner, a relatively quick additive change between successive batches of filaments 16 is possible (i.e., to allow for changes in additive recipe to be realized from one filament batch to another). In addition, such an inlet location for the additive concentrates also allows for a wide range of processing flexibility to be achieved. For example, the additive pastes from tanks 18 a, 18 b, 18 c and/or 18 d may be mixed with the entirety of polymeric host material supplied via line 32 so that all of the filaments 16 have the same color. Alternatively, the distribution/mixing section 14 c of the spin pack assembly 14 may be so provided to split the flow of polymeric host material with one or more of the additive concentrate pastes being mixed with one or more of such split flows to achieve, for example, multiple differently colored filament groups which may remain segregated to form single color yarns or may be combined to form multicolor yarns, such as in a heather yarn. In addition, several additives may be mixed with the host polymer so that, for example, single color yarns having multiple additive concentrations therein may be produced from the same spinning equipment. Similarly, one or more additive concentrate pastes may be mixed with split flows of polymeric host material within the distribution/mixing section 14 c of the spin pack assembly 14 to achieve multifilamentary yarns having differently colored filaments (e.g., as may be desired to produce yarns having a heathered appearance).

Although accompanying FIG. 1 (and the description above) shows the additive concentrate system pastes being preferably introduced into the melt flow of polymeric host material directly into the spin pack assembly 14 at a location between the polymer filter section 14 a and the spinneret 14 b, it will be understood that the pastes may be incorporated into the melt flow of polymeric host material at any location upstream of the spinneret 14 b. Thus, for example, the additive system pastes may be incorporated into the melt flow of polymeric host material by feeding through an injection port associated with the extruder 12 and/or through a port in line 32. Thus, for example, the additive system pastes may be introduced to the polymeric host material at or downstream of the extruder throat, but upstream of the spinneret 14 b.

Different batches of colored filaments 16 may thus be produced continuously by simply changing the recipe in the controller LPC and allowing a sufficient time interval to elapse to ensure that any residual amounts of the additive concentrate system pastes associated with the prior recipe have been purged from the spin pack assembly 14. While some off-specification filament will ensue during the change-over to the new recipe, its economic impact is small by comparison to complete shut-down of the spinning operation. Furthermore, since relatively small amounts of the additive concentrate system pastes will residually be present in the spin pack assembly 14 at the time of recipe change-over, only a relatively short time interval is needed to purge the spin pack assembly of the prior additive recipe and begin producing filaments pigmented with the new recipe.

III. EXAMPLES

The following nonlimiting examples will provide a further understanding of this invention.

In this regard, carpet samples formed of filaments colored in accordance with the present invention and filaments colored in accordance with conventional extruder melt-blending techniques were tested according to the following procedures and, where applicable, a subjective rating scale of between 1 to 5 was utilized (5 being the best rating):

Yarn Degradation: Data representative of yarn strength/elongation before and after 100, 200 and 300 hours ultraviolet radiation exposure according to AATCC Test Method 16-1993, Option E.

Colorfastness: Yarn color/visual data after 100, 200 and 300 hours ultraviolet radiation exposure according to AATCC Test Method 16-1993, Option E.

Taber Abrasion Test: ASTM D3884-92.

Crocking: AATCC Test Method 8-1989.

Exposure to 50% Bleach: Carpet samples were cut into two 4.5″×9″ squares. 25 ml of a bleach solution containing about 2.6% sodium hypochlorite (50% Clorox® brand bleach and water) was poured into the center of one sample to form a test region approximately 2″ in diameter. The sample was allowed to air dry for 24 hours after which it was rinsed with a hot detergent/water solution containing 12 parts water and 1 part detergent. The rinsed sample was air dried for 24 hours after which it was visually rated on a scale of 1 to 5 against the untreated sample using AATCC Gray Scale in a Macbeth light booth (daylight setting).

Visual Grades After Exposure to Ozone: AATCC Test Method 129-1990.

Visual Grades After Exposure to NO₂: AATCC Test Method 164-1992.

Dry Heat Exposure: Samples are heated in a laboratory oven (1600 Wafts, Model No. OV-490, Blue M. Electric Co., Blue Island, Ill.) at 280° F. and 320° F. and removed after ten minutes. The samples are allowed to cool and visually rated on a scale of 1 to 5 using MTCC Gray Scale.

Tetrapod Wear: ASTM D5251-92.

Hunter Green Purge Value: The additive concentrate systems of the present invention achieve a Hunter Green Purge Value (“HGPV”) of between about 0.10 to about 1.40 sec/cm³ more preferably, between about 0.50 to about 1.40 sec/cm³, and most preferably between about 0.80 to about 1.05 sec/cm³. In this regard, HGPV is the time, in seconds, per unit volume, in cubic centimeters, of the spinning system required for at least 90% of melt-spun Hunter Green nylon-6 filaments to achieve a CIE L* value of about 63 or greater at a system throughput of 217 g/min. Hunter Green nylon-6 polymer employed to determine HGPV was prepared as described in Example 10 below.

Example 1

Dispersant-coated pigment particles were prepared using the components noted in Table A below. The components were blended using a high shear dissolver type mixer. A water soluble polyamide dispersant polymer (C-68 manufactured by BASF Corporation in accordance with U.S. Pat. No. 3,846,507 except that poly(E-caprolactam) was used as a starting material instead of E-caprolactam) was first dissolved in water to prepare a 25 percent stock solution. Pigment dispersions were then bead-milled with 2 mm glass beads for three passes through the mill and were thereafter spray-dried. The dispersions were spray-dried using a Niro FSD-Pilot unit, which had a 1.5 meter diameter, 0.8 meters cylinder height, 400 cone, and a fluidized bed collector at the bottom of the chamber. Dispersions were fed into the dryer with a two-fluid, externally-mixed nozzle. The spray-dryer was run with 253-263° C. inlet and 67-103° C. outlet temperatures. The spray-dried powder tended to be dusty, and thus a fluidized bed collector was used to increase agglomerate size and thereby reduce the dust.

TABLE A % Pigment in % Dispersant in Aqueous Aqueous Pigment Dispersion Dispersion Inorganic Yellow 32.5 13.0 Organic Blue 20.0 15.0 Organic Red 20.0 15.0 Inorganic Tan 30.0 12.0 Organic Green 25.0 12.5 Organic Black 20.0 15.0 White/Stabilizer 32.5 13.0

Example 2

Example 1 was repeated except that a water-dispersible polyester (LB-100 from Eastman Chemical Products, Inc.) was used as the dispersant polymer in the amounts noted in Table B below. Unlike Example 1 above, all dispersions according to this Example 2 contained 5.0% of a polyoxypropylene-polyoxyethylene block copolymer surfactant (Pluronic® 25R2 surfactant from BASF Corporation). Sprayried dispersions using LB-100 as the dispersant were not dusty, and were prepared using the Niro spray-dryer which was not equipped with a fluidized bed collector. The Niro spray dryer was run with 220° C. inlet and 80-95° C. outlet temperatures. These dispersions were fed into a rotary wheel type atomizer running at 18,500 rpm.

TABLE B % Pigment in % Dispersant in Aqueous Aqueous Pigment Dispersion Dispersion Organic Blue 27.5 20.6 Organic Red 27.5 20.6 Inorganic Tan 32.5 13.0 Organic Green 32.5 24.7 Organic Black 25.0 18.7 White 40.0 16.0 White/Stabilizer 40.0 16.0

Example 3

The additive concentrate pastes in Table C below were prepared by first melting at 150° C. 50-60% of the required copolyamide carrier polymer (Vestamelt 722 from Hüjls America Inc.). The spray-dried powders obtained according to Example 1 above were then bag-blended in desired ratios to achieve desired final colors and stirred into the molten carrier polymer. The balance of the carrier polymer needed was then added and stirred into the concentrate blend formulation. The spray-dried powders tended to form large agglomerates which did not disperse without extended agitation. Thus, the blends were stirred overnight (approximately 10 to 12 hours) prior to yarn extrusion.

The white/stabilizer pigments used in the blended pigment ratios for all final colors, except Gray and Light Gray, were not the spray dried coated pigments obtained according to Example 1. Instead, the white/stabilizer pigments were compounded with Vestamelt 722 polymer using a vented twin screw compounding extruder to obtain chip concentrates having 25 wt. % of white pigment and 25 wt. % stabilizer. The chip concentrates of such white/stabilizer pigments were then blended in desired ratios with certain of the spray-dried pigments obtained in Example 1 to achieve the final colors noted below in Table C.

TABLE C Total % Pigment in Final Color Paste Light Gray 13.9 Gray 9.3 Black 20.4 Light Green 20.0 Purple 25.3 Blue 19.0 Light Tan 19.8 Mauve 18.7 Green 19.0 Brown 19.7

Example 4

The additive concentrate pastes in Table D below were prepared following the procedures of Example 3 above, except that the spray-dried powders obtained from Example 2 were used, and the carrier was polycaprolactone. Unlike Example 3, no compounded chips of white/stabilizer pigments were used.

TABLE D Total % Pigment in Final Color Paste Light Gray 37.0 Gray 37.8 Black 34.0 Light Green 39.0 Purple 35.5 Blue 34.8 Light Tan 35.0 Mauve 30.5 Green 34.9 Brown 37.7

Example 5

A Barmag 6E extruder was used for filament yarn extrusion with the additive concentrate pastes in Table C being fed downstream of the extruder at around 150° C. in desired ratios to achieve the filament color noted below in Table E. The resulting melt-spun filament yarns were 6-hole pentagonal cross-section, 715+/−15 denier, and 14 filaments/end. Eight ends of these undrawn yarns were combined during draw texturing to prepare 2250/112 denier yarns which were then two-ply cable-twisted to make 4500/224 denier carpet yarns. The carpet yarns were then tufted into 1/10 gauge, 26 ounces/square yard, {fraction (3/16)}″ pile height level loop carpets.

The carpets were then tested to determine various physical properties using the testing methods and techniques described previously. The results of such testing are tabulated below in Tables 1-4 and are presented in comparison to carpets formed of “control” filaments of matching color. The “control” filaments were made using conventional compounded pigment chips which were melt-blended with the polymeric host chip in an extruder, with the melt-blend then being fed to the spinneret.

TABLE E Additive Concentrate % Additive Paste Components Concentrate Final Color Other Than Stabilizer Paste in Filament Light Gray black, white, green, blue 1.4 Gray black, white, blue, red 2.6 Black black, white 3.8 Light Green black, white, green, tan 1.4 Purple black, white, blue, red 2.6 Blue black, white, blue, red 2.8 Light Tan black, green, tan 1.7 Mauve black, blue, red 2.8 Green black, green, blue 4.2 Brown black, white, red, tan 6.5

TABLE 1 Carpet physical properties after ultraviolet exposure. Test samples made with C-68 Yarn Degradation Colorfastness Pounds Break Strength Visual Ratings (1-5) Sample Original 100 hours 200 hours 300 hours 100 hours 200 hours 300 hours TAN_CTRL_A 35.5 33.8 34.4 32.5 5 4-5 4-5 TAN_V722 34.8 34.3 32.65 33.15 5 4 3-4 LT_GRAY_CTRL_A 34.3 35.1 35.3 33.62 4-5 3-4 3 LI_GRAY_V722 35.9 32.4 32.85 31.7 4-5 3 2-3 LT_GREEN_CTRL_A 36 34.8 35.3 34.2 5 4 3-4 LT_GREEN_V722 33.1 33 32 33.05 5 4-5 4-5 GRAY_CTRL_A 35.93 34.3 32.2 30.35 4-5 3-4 3-4 GRAY_V722 33.3 31.9 30.15 29.85 5 4 3-4 BLACK_CTRL_A 33.05 30.6 28.2 26.55 5 5 4-5 BLACK_V722 31.9 30.9 30.81 31.11 5 5 5 BROWN_CTRL_A 34.93 33.8 33.22 31.87 5 5 4-5 BROWN_V722 31.64 31.1 30.7 31.31 5 5 4-5 GREEN_CTRL_A 34.48 31.7 33 32.76 5 5 5 GREEN_V722 33.7 32.3 32.33 31.72 5 4-5 4-5 BLUE_CTRL_A 33.96 32.5 31.55 30.68 5 4-5 4-5 BLUE_V722 33.6 32.3 31.2 31.8 5 4-5 4-5 PURPLE_CTRL_A 33.73 31.3 27.25 25.82 5 5 4-5 PURPLE_V722 31.98 32.2 30.38 30.28 5 5 4-5 MAUVE_CTRL_A 33.8 33.4 30.8 28.75 5 5 4-5 MAUVE_V722 32.2 30.9 29.9 27.35 5 5 4-5

TABLE 2 Carpet visual ratings after Taber wear, crock testing, and bleach exposure. Test samples made with C-68 Taber Abrasion Test Grams Weight Loss After: Crocking Exposure 1000 cycles 2000 cycles Dry Wet to 50% Bleach TAN_CTRL_A 0.077 0.122 5 5 4 TAN_V722 0.0592 0.1069 5 5 4-5 LT_GRAY_CTRL_A 0.0841 0.1179 5 5 4-5 LT_GRAY_V722 0.0303 0.0587 5 5 3-4 LT_GREEN_CTRL_A 0.0793 0.1138 5 5 4-5 LT_GREEN_V722 0.0666 0.0987 5 5 5 GRAY_CTRL_A 0.0448 0.0845 5 5 4-5 GRAY_V722 0.0792 0.1312 5 5 4-5 BLACK_CTRL_A 0.0594 0.0847 5 5 5 BLACK_V722 0.05 0.0968 5 5 4-5 BROWN_CTRL_A 0.0461 0.0853 5 5 4-5 BROWN_V722 0.0578 0.1013 5 5 4-5 GREEN_CTRL_A 0.0513 0.0963 5 5 4-5 GREEN_V722 0.0713 0.1153 5 5 4-5 BLUE_CTRL_A 0.0797 0.1213 5 5 4 BLUE_V722 0.077 0.1139 5 5 4-5 PURPLE_CTRL_A 0.0616 0.0998 5 5 5 PURPLE_V722 0.0957 0.14 5 5 4-5 MAUVE_CTRL_A 0.0263 0.0471 5 5 4-5 MAUVE_V722 0.0392 0.0879 5 5 4-5

TABLE 3 Carpet visual ratings after ozone and nitrogen oxides exposure. Test samples made with C-68 Visual Grades After Visual Grades After Exposure to Ozone Exposure to NO2 3 cycles 8 cycles 3 cycles 8 cycles TAN_CTRL 4-5 4-5 4-5 4-5 TAN_V722 4-5 4-5 4-5 4 LT_GRAY_CTRL 4-5 4 3-4 3 LT_GRAY_V722 4-5 4 3-4 3 LT_GREEN_CTRL 5 5 4-5 4 LT_GREEN_V722 5 4-5 4-5 4 GRAY_CTRL 4-5 4-5 5 4-5 GRAY_V722 4-5 4 4-5 3-4 BLACK_CTRL 5 4-5 5 5 BLACK_V722 5 4-5 5 5 BROWN_CTRL 5 4-5 5 4-5 BROWN_V722 5 4-5 5 4-5 GREEN_CTRL 5 5 5 4-5 GREEN_V722 5 5 4-5 4-5 BLUE_CTRL 5 4-5 4-5 4 BLUE_V722 5 4-5 4-5 4-5 PURPLE_CTRL 5 4-5 5 4-5 PURPLE_V722 5 5 5 5 MAUVE_CTRL 5 4-5 5 5 MAUVE_V722 5 5 5 4-5

TABLE 4 Carpet visual ratings after exposure to dry heat and Tetrapod wear. Test samples made with C-68 Dry Heat Exposure 500 K in Tetrapod 280° F. 320° F. Stair End TAN_CTRL_A 5 4-5 4 4 TAN_V722 5 4-5 3 3-4 LT_GRAY_CTRL_A 4-5 4 3-4 3-4 LT_GRAY_V722 4 3 3-4 4 LT_GREEN CTRL_A 4-5 4 3-4 3-4 LT_GREEN_V722 4-5 4 3 3-4 GRAY_CTRL_A 5 4-5 4 4 GRAY_V722 4-5 3-4 3 3-4 BLACK_CTRL_A 5 4-5 4 4-5 BLACK_V722 5 5 4 4 BROWN_CTRL_A 5 4-5 3-4 4 BROWN_V722 5 4-5 4 4 GREEN_CTRL_A 5 4-5 2-3 3-4 GREEN_V722 5 4-5 2 3 BLUE_CTRL_A 5 4-5 3-4 4 BLUE_V722 5 4-5 3 3-4 PURPLE_CTRL_A 5 4-5 3-4 4 PURPLE_V722 5 4-5 3-4 3-4 MAUVE_CTRL_A 5 4-5 4 4 MAUVE_V722 5 4-5 3-4 4

Example 6

Example 5 was repeated except that the additive concentrate pastes of Table D were fed at the extruder throat at ambient temperature (about 20° C.). The paste components and the amount of paste in the filaments are noted below in Table F. The resulting filaments were formed into carpets and tested similar to Example 5. The results appear in Tables 5-8 below.

TABLE F Additive Concentrate % Additive Paste Components Concentrate Final Color Other Than Stabilizer Paste in Filament Light Gray black, white, green, blue 0.6 Gray black, white, blue, red 0.7 Black black, white 2.2 Light Green black, white, green, tan 0.8 Purple black, white, blue, red 2.0 Blue black, white, blue, red 1.6 Light Tan biack, green, tan 1.0 Mauve black, blue, red 1.9 Green black, green, blue 2.2 Brown black, white, red, tan 3.6

TABLE 5 Carpet physical properties after ultraviolet exposure. Test samples made with LB-100 Yarn Degradation Colorfastness Pounds Break Strength Visual Ratings (1-5) Sample Original 100 hours 200 hours 300 hours 100 hours 200 hours 300 hours TAN_CTRL_B 36.06 36 35.2 32.85 5 4-5 4-5 TAN_PCL 35.08 34.45 35 33.4 5 4-5 4-5 LT_GRAY_CTRL_B 36.13 35.98 35.8 34.8 3 2-3 2-3 LT_GRAY_PCL 35.97 35.95 34.35 33.95 3-4 2-3 2-3 LT_GREEN_CTRL_B 36.7 36.15 35.1 32.85 4-5 4 3 LT_GREEN_PCL 35.93 35.01 34.05 32.95 5 4-5 4 GRAY_CTRL_B 36.43 36.03 35.1 35.2 5 5 4-5 GRAY_PCL 35.95 34.71 32.25 31.2 5 4 4 BLACK_CTRL_B 32.56 30 28.21 22.96 5 4-5 4-5 BLACK_PCL 31.25 30.85 30.9 28.08 5 4-5 4-5 GREEN_CTRL_B 33.15 32.05 31.6 29.8 5 4-5 4-5 GREEN_PCL 32.83 32.41 32.5 30.45 5 4-5 4-5 BLUE_CTRL_B 34.5 32.8 31.67 29.5 4-5 4-5 4 BLUE_PCL 34.78 33.7 34.21 32.35 5 4-5 4-5 PURPLE_CTRL_B 33.52 32.33 27.95 24.1 5 4-5 4 PURPLE_PCL 33.68 32.55 32.25 29.25 4-5 4-5 4

TABLE 6 Carpet visual ratings after Taber wear, crock testing, and bleach exposure. Test samples made with LB-100 Taber Abrasion Test Grams Weight Loss After Crocking Exposure 1000 cycles 2000 cycles Dry Wet to 50% Bleach TAN_CTRL_B 0.033 0.0661 5 5 5 TAN_PCL 0.0252 0.0487 5 5 4-5 LT_GRAY_CTRL_B 0.0365 0.0664 5 5 3-4 LT_GRAY_PCL 0.0018 0.0234 5 5 3-4 LT_GREEN_CTRL_B 0.0186 0.0394 5 5 4-5 LT_GREEN_PCL 0.013 0.0426 5 5 5 GRAY_CTRL_B 0.0427 0.0529 5 5 4-5 GRAY_PCL 0.0297 0.0608 5 5 4 BLACK_CTRL_B 0.0905 0.1216 5 5 4-5 BLACK_PCL 0.1323 0.1898 5 5 4-5 GREEN_CTRL_B 0.0561 0.0874 5 5 4-5 GREEN_PCL 0.0392 0.0668 5 5 4-5 BLUE_CTRL_B 0.065 0.0987 5 5 4-5 BLUE_PCL 0.0693 0.1297 5 5 4-5 PURPLE_CTRL_B 0.0719 0.1082 5 5 4 PURPLE_PCL 0.0887 0.1289 5 5 4

TABLE 7 Carpet visual ratings after ozone and nitrogen oxides exposure. Test samples made with LB-100 Visual Grades After Visual Grades After Exposure to Ozone Exposure to NO2 3 cycles 8 cycles 3 cycles 8 cycles TAN_CTRL_B 4-5 4 4-5 4 TAN_PCL 4-5 4-5 4-5 4-5 LT_GRAY_CTRL_B 4-5 4 4 3 LT_GRAY_PCL 4 3-4 4 3-4 LT GREEN_CTRL_B 4-5 4-5 4 4 LT_GREEN_PCL 4-5 4-5 4-5 4-5 GRAY_CTRL_B 4-5 4-5 4 4 GRAY_PCL 4-5 4-5 4-5 4-5 BLACK_CTRL_B 5 4-5 5 4-5 BLACK_PCL 5 4-5 5 4-5 GREEN_CTRL_B 5 4-5 5 4-5 GREEN_PCL 4-5 4 5 4 BLUE_CTRL_B 4-5 4 4-5 4 BLUE_PCL 4-5 4 4-5 4-5 PURPLE_CTRL_B 4-5 4 4-5 4 PURPLE_PCL 4-5 4 4-5 4

TABLE 8 Carpet visual ratings after exposure to dry heat and Tetrapod wear. Test Samples made with LB-100 Dry Heat Exposure 500 K in Tetrapod 280° F. 320° F. Stair End TAN_CTRL_B 4-5 4 3 3 TAN_PCL 4-5 4 3 3 LT GRAY_CTRL_B 4-5 3 3 3 LT_GRAY_PCL 4-5 3 3 3 LT GREEN_CTRL_B 4-5 3-4 3 3 LT_GREEN_PCL 4-5 4 3 3 GRAY_CTRL_B 4-5 4 3 3 GRAY_PCL 4-5 4 3 3 BLACK_CTRL_B 5 5 3-4 4 BLACK_PCL 5 5 3-4 3-4 GREEN_CTRL_B 5 4-5 2-3 3-4 GREEN_PCL 5 4-5 3-4 3-4 BLUE_CTRL_B 5 4-5 3-4 3-4 BLUE_PCL 4-5 4 3-4 3-4 PURPLE_CTRL_B 4-5 4 3-4 3-4 PURPLE_PCL 4-5 4 3-4 3-4

The data in Tables 1-8 above demonstrate that the performance properties of carpet yarns made from pigmented filaments of this invention are comparable to carpet yarns which are colored according to the conventional practice of melt-blending pigmented chips with base polymer chips. It is surprising that the incorporation of the low molecular-weight polymer as the carrier in the dispersible additive did not affect either the breaking strength or elongation of the pigmented filaments of this invention when compared to conventional melt-colored filaments.

Example 7

A tan additive concentrate paste was formed by direct blending of 40 wt. % tan pigment particles, 8 wt. % of polyethylene glycol p-octyl phenyl ether (Triton X-100) dispersant, and 52 wt. % polycaprolactone. The resulting additive concentrate paste was preheated to approximately 140° C. and exhibited a viscosity of between 2000 to 4000 cP. The paste was pumped directly into a spin pack assembly at a location downstream of the polymer filter but upstream of the spinneret orifices (58 hole asymmetrical trilobal). The additive concentrate paste was mixed with the nylon-6 polymeric host material within the spin pack assembly at a rate of between about 6.0 g/min (to obtain about 0.8-1.1 wt. % pigment in the resulting melt-spun filaments) to about 7.3 g/min (to obtain about 1.1-1.5 wt. % pigment in the resulting melt-spun filaments). The resulting melt-spun filaments had a uniformly colored appearance along the lengthwise extent as viewed with an unaided eye. Microscopic views of filament cross-sections revealed that substantially homogenous to somewhat striated mixing had occurred in dependence upon the injection rate of the additive paste.

Example 8

Example 2 was repeated to produce the dispersible additives noted in Table F below:

TABLE F % Pigment in % Dispersant in Aqueous Aqueous Pigment Dispersion Dispersion Anatase TiO₂ 37.5 15.0 Red 149 27.5 20.6 Green 7 27.5 20.6 Black 6 25.0 18.7 Blue 15 27.5 20.6 Brown 11 32.5 13.0 Red 101 20.0 13.0 Red 179 35.0 17.5 Violet 29 20.0 12.0 Red 101 30.0 11.2 Brown 24 32.5 13.0 Blue 60 25.0 12.5 Red 202 27.5 20.6

The additive concentrate pastes in Table G below were prepared following the procedures of Example 3 above, except that the spray-dried powders of Table F above were used, and the carrier was polycaprolactone.

TABLE G % Spray Dried Pigment Powder in Paste Anatase TiO₂ 57.21 Red 149 57.44 Green 7 57.44 Black 6 57.44 Blue 15 57.44 Brown 11 57.21 Red 101 57.21 Red 179 52.50 Violet 29 57.44 Red 101 57.21 Brown 24 57.21 Blue 60 57.21 Red 202 57.21

Example 9

In order to investigate the effectiveness of employing spray-dried additive powders in accordance with the present invention, an aqueous C.I. pigment black 6 dispersion using LB-100 as the dispersant was ball-milled in a Chicago Boiler five-liter horizontal Dyno-Mill loaded with 4.25 liters of 1.0-1.3 mm glass beads and running at 1705 rpm. The aqueous dispersion was spray-dried in a Niro Utility Spray Dryer having a rotary atomizer running at 24,350 rpm. The inlet air temperature was 220° C. at about 220 cfm. The dispersion feed rate was adjusted to achieve a discharge air temperature of 90° C. The resulting spray dried dispersible pigment particles were then blended with polycaprolactone as the carrier to form a paste such that 20 wt. % of the black pigment was present in the resulting paste. The viscosity (centipoise) of the paste was then investigated as a function of shear rate (sec⁻¹) with the results being present in Table H (the “Spray Dry/Disperse” sample).

By way of comparison, 20 wt. % of the same black pigment (C.I. pigment black 6) was dispersed directly in polycaprolactone carrier without the benefit of being spray dried with LB-100 dispersant. The viscosity (centipoise) of the dispersion was also investigated as a function of shear rate (sec⁻¹) with the results being present in Table H below (the “Direct Disperse” sample).

TABLE H Spray Dry/Disperse Direct Disperse Shear Rate Viscosity Shear Rate Viscosity (sec⁻¹) (cps) (sec⁻¹) (cps) 1.4 8148 0.6 50130 2.4 5729 1.2 31290 4.2 4303 3.0 14940 7.3 3466 6.0 11440 12.6 2744 12.0 6291 21.8 2385 24.0 4825

The data above demonstrate that, at the same pigment loadings in the dispersions, significantly lower viscosities ensue at the same shear rates for spray-dried pigments. Thus, at comparable shear rate, greater pigment loadings are possible for the spray-dried pigments without adversely affecting processing conditions. As a result, therefore, the dispersible additive pastes of this invention which include spray-dried pigments can be incorporated into the host polymeric materials in lesser amounts as compared to direct dispersed pigments in order to achieve comparable pigment properties.

Example 10

Hunter Green Purge Values

Green 7, Black 6, Blue 15 and White (anatase TiO₂) pastes were prepared according to Example 8, above. Specifically, batches of 200 pounds of each paste were prepared using a mixing profile which began with 30 seconds at a tip speed of 10 m/sec, followed by 3 minutes at 20 m/sec, followed by a discharge period of 45 seconds at 6-8 m/sec.

A copper stabilizer paste was also prepared by charging the mixer with 125 pounds of copper stabilizer and 125 pounds of polycaprolactone. The mixing profile for the copper stabilizer paste began with 10 m/sec tip speed for 2 minutes followed by 10 minutes at 40 m/sec. The copper stabilizer paste was allowed to cool to 125° F. by dropping the mixer tip speed to 10 m/sec and circulation of cooling water through the mixer jacket. After the temperature had dropped, the copper stabilizer paste was discharged at 6-8 m/sec tip speed.

Hunter Green color pastes were prepared by charging the following components and polycaprolactone liquid polymer into a Henschel FM-200 high intensity mixer (all percentages being the weight percent of the components in the paste blend):

(1) Copper Stabilizer Paste: 0.5-1.0 wt. %

(2) Green 7 Paste: 50-60 wt. %

(3) Black 6 Paste: 5-10 wt. %

(4) Blue 15 Paste: 10-15 wt. %

(5) White (anatase TiO₂) Paste: Balance to bring Hunter Green paste blend to 100 wt. %

In order to determine the HGPV, the Hunter Green paste is injected into the host polymer (e.g., nylon 6) at 2.7 wt. % to achieve Hunter Green filaments. Injection of the Hunter Green paste is stopped and the time in seconds per unit spinning system volume, in cubic centimeters, is determined when at least 90% of the filaments achieve a CIE L* value of 63 or greater at a system throughput of 217 g/min. 

What is claimed is:
 1. A method of making pigmented filaments comprising: (i) supplying a melt flow of a melt-spinnable polymeric host material to spinneret orifices; (ii) incorporating within at least a portion of the melt flow of polymeric host material upstream of the spinneret orifices, a dispersible non-aqueous additive comprised of (1) dispersant-coated pigment particles, formed of solid pigment particles coated with a water-soluble/dispersible dispersant, which are dispersed in (2) a nonaqueous polycaprolactone carrier which is liquid at room temperature to form a mixture of the polymeric host material and the dispersible non-aqueous additive; wherein the dispersant is selected from the group consisting essentially of water soluble/dispersible polyamides and copolymers thereof, water-soluble/dispersible polyesters and copolymers thereof, water soluble/dispersible alkylene oxide polymers and copolymers thereof, water soluble/dispersible polyolefins and copolymers thereof, and mixtures thereof, and wherein the dispersant is soluble in the polymeric host material to an extent of at least about 5 wt. %, based on the total weight of the dispersant and polymeric host material and the dispersant is substantally insoluble with the polycaprolactone carrier at a temperature which is less than about the melt temperature of the polymeric host material minus 50° C., and then (iii) extruding a melt of the mixture of the polymeric host material and the non-aqueous dispersible additive through the spinneret orifices to form pigmented filaments.
 2. The method of claim 1, wherein the dispersant is a water soluble material that is normally solid when dehydrated.
 3. The method as in claim 1, or 2, wherein the dispersant is a sulphonated polyamide or polyester.
 4. The method as in claim 1, wherein step (ii) is practiced so as to incorporate said dispersible additive in said polymeric host material at a substantially constant rate.
 5. The method as in claim 1, wherein step (ii) is practiced so as to incorporate said dispersible additive in said polymeric host material at a randomly or constantly varied rate.
 6. The method as in claim 1, wherein step (ii) is practiced so as to incorporate the dispersible additive in an amount between about 0.01 to about 15% by weight of the mixture.
 7. The method as in claim 1, wherein the dispersible additive has a viscosity of between about 500 cP to about 500,000 cP at a temperature between about 20° C. to about 200° C.
 8. An additive-containing filament formed of a polymeric host material, and containing non-aqueous additive system dispersed throughout at least a portion of the polymeric host material, wherein said non-aqueous additive system comprises (1) dispersant-coated pigment particles, formed of solid pigment particles coated with a water-soluble/dispersible dispersant, which are dispersed in (2) a nonaqueous polycaprolactone carrier which is liquid at room temperature, wherein the dispersant is selected from the group consisting essentially of water-soluble/dispersible polyamides and copolymers thereof, water soluble/dispersible polyesters and copolymers thereof, water soluble/dispersible alkylene oxide polymers and copolymers thereof, water soluble/dispersible polyoletins and copolymers thereof, and mixtures thereof, and wherein the dispersant is soluble in the polymeric host material to an extent of at least about 5 wt. %, based an the total weight of the dispersant and polymeric host material and the dispersant is substantially insoluble with the polycaprolactone carder at a temperature which is less than about the melt temperature of the polymeric host material minus 50° C.
 9. An additive-containing filament as in claim 8, wherein the dispersant is a water soluble material that is normally solid when dehydrated.
 10. An additive-containing filament as in claim 8, wherein the dispersant is a sulphonated polyamide or polyester.
 11. An additive-containing filament as in claim 8, further comprising a co-dispersant.
 12. An additive-containing filament as in claim 11, wherein the co-dispersant is selected from the group consisting of polyethylene glycol p-octyl phenyl ether, polyoxypropylene/ethylene block copolymers, alkoxylated diamines, sodium lauryl sulfate and cationic dispersants.
 13. An additive-containing filament as in claim 8, wherein the polymeric carrier is normally liquid.
 14. An additive-containing filament formed of a polymeric host material, and containing a non-aqueous additive system comprising dispersant-coated pigments in a nonaqueous polycaprolactone carrier which is liquid at room temperature dispersed throughout at least a portion of the polymeric host material.
 15. An additive-containing filament as in claim 8, wherein the pigments are colorant particles having a mean particle size of less than 10 μm.
 16. An additive-containing filament as in claim 8, wherein the pigments are present in an amount between about 5 to about 75% by weight.
 17. The additive-containing filament as in 8, having a Munsell Value between about 2.5/ to about 8.5/ and a Munsell Chroma greater than about /0.5.
 18. A yarn containing a filament of any one of claims 8, 9, 10, 11, 12, 13, 14, 15, 16 or
 17. 19. A yarn containing a filament formed of a composition which comprises a polymeric host material, and a non-aqueous additive system dispersed throughout at least a portion of the polymeric host material, wherein said non-aqueous additive system comprises (1) dispersant-coated pigment particles, formed of solid pigment particles coated with a water-soluble/dispersible dispersant, which are dispersed in (2) a nonaqueous polycaprotactone carder which is liquid at room temperature, wherein the dispersant is selected from the group consisting essentially of water soluble/dispersible polyamides and copolymers thereof, water-soluble/dispersible polyesters and copolymers thereof, water soluble/dispersible alkylene oxide polymers and copolymers thereof, water soluble/dispersible polyolefins and copolymers thereof, and mixtures thereof, and wherein the dispersant is soluble in the polymeric host material to an extent of at least about 5 wt. %, based on the total weight of the dispersant and polymeric host material and the dispersant is substantially insoluble with the polycaprolactone carrier at a temperature which is less than about the melt temperature of the polymeric host material minus 50° C.
 20. The yarn of claim 19, wherein the polymeric host material is selected from the group consisting of normally solid, melt-processable, synthetic thermoplastic polymers, copolymers and mixtures of such polymers and copolymers.
 21. The yarn of claim 19, wherein the polymeric host material is selected from the group consisting of polyamides, polyesters, polyoletins and polyurethanes.
 22. The yarn of claim 19, wherein the polymeric host material is nylon-6.
 23. The yarn of claim 19, wherein the dispersant is a water-soluble sulphonated polyamide and/or polyester.
 24. The yarn of claim 19, wherein the composition further comprises a co-dispersant selected from the group consisting of polyethylene glycol p-octyl phenyl ether, polyoxypropylene/ethylene block copolymers, alkoxylated diamines, sodium lauryl sulfate and cationic dispersants.
 25. The yarn of claim 19, wherein the polymeric carrier is normally liquid.
 26. The yarn of claim 19, wherein the pigment particles are colorant particles having a mean particle size of less than 10 μm.
 27. A carpet which includes a yarn of any one of claims 19, 20, 21, 22, 23, 24, 25 or
 26. 